EP2663742B1 - Procédé et installation permettant la récupération d'énergie à partir de la biomasse et des déchets combustibles, en particulier des matières premières renouvelables, ainsi que leur carbonisation - Google Patents

Procédé et installation permettant la récupération d'énergie à partir de la biomasse et des déchets combustibles, en particulier des matières premières renouvelables, ainsi que leur carbonisation Download PDF

Info

Publication number
EP2663742B1
EP2663742B1 EP11709323.7A EP11709323A EP2663742B1 EP 2663742 B1 EP2663742 B1 EP 2663742B1 EP 11709323 A EP11709323 A EP 11709323A EP 2663742 B1 EP2663742 B1 EP 2663742B1
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
biomass
reactor
exhaust gases
plant
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Not-in-force
Application number
EP11709323.7A
Other languages
German (de)
English (en)
Other versions
EP2663742A2 (fr
Inventor
Jan GLADKI
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Gerhard Rieder GmbH
Original Assignee
Gerhard Rieder GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Gerhard Rieder GmbH filed Critical Gerhard Rieder GmbH
Publication of EP2663742A2 publication Critical patent/EP2663742A2/fr
Application granted granted Critical
Publication of EP2663742B1 publication Critical patent/EP2663742B1/fr
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05D—INORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C; FERTILISERS PRODUCING CARBON DIOXIDE
    • C05D9/00—Other inorganic fertilisers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/44—Solid fuels essentially based on materials of non-mineral origin on vegetable substances
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C10L9/083—Torrefaction
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F01K3/18—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
    • F01K3/188—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters using heat from a specified chemical reaction
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/14—Combined heat and power generation [CHP]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the invention relates to a plant and a method for energy recovery from biomass and combustible waste, in particular from renewable raw materials and for carbonization of these substances.
  • the invention is for the production of electrical and thermal energy, of solid fuels, referred to as biochar, as well as of agriculturally usable natural fertilizer. It is in addition to the material and energetic use of renewable resources for the production of biochar and energy from biological waste of the food industry and the industrial processing of fruits and vegetables, sorted municipal waste, from deposits of sewage treatment plants, from animal biomass, so from bone meal, and from all other solid biological alternative and waste materials.
  • the Polish patent PL 179 990 discloses a plant for the pyrolysis of solid waste having a rotary kiln in front of which there is a device for preheating solids. It is connected by a dense rotatable intermediate link with the rotary kiln.
  • the device for preheating consists of a horizontal tube in which a transport channel for solid waste is housed, which is fed with a collector.
  • the device has two heating zones, which are equipped with a heating jacket. In the first zone, the waste is preheated to a temperature of 50 ° C to 150 ° C. In the second zone, the temperature reaches from 100 ° C to 500 ° C.
  • the waste feeds the inclined rotary kiln in the gravitational mode and forms in its lower part a deposit which shifts in the direction of the kiln slope as a result of the revolutions.
  • the waste is processed at a temperature of 150 ° C to 900 ° C.
  • the DE 20 2006 016 U1 describes a plant for the gasification of biomass with a continuous entry, subsequent comminution and gas purification, wherein in a screw extruder by a Zerfaserungsschnecke by the addition of water vapor and / or pure oxygen under a pressure of 25 bar to 30 bar at temperatures of 100 ° C to 250 ° C decomposes the biomass and after supplying oxygen in a subsequent combustion chamber at about 900 ° C, the gasification takes place and the resulting gas is purified by means of metallic membrane filters and catalytically.
  • the DE 10 2008 004 732 A1 discloses a method and apparatus for hydrothermal carbonization of biomass.
  • Biomass is converted with water and at least one catalyst in a pressure vessel by increasing the temperature and / or pressure in coal, oil and / or the like related materials being provided in fluidic connection a device for disorganization of the biomass before and / or in the pressure vessel.
  • a multi-reactor process for the thermal carbonation of biomass is disclosed DE 10 2008 056 006 A1 ,
  • the biomass is converted by this method with water and a catalyst in cascade pressure vessels by increasing the temperature and / or pressure in coal, oil and related substances.
  • the product consisting of biomass, water and catalyst and preheated contents is controlled in a holding process so that these components react with each other and then removed the reaction products from the reactor.
  • the plant consists of containers for the biomass and the waste fuels, equipment for comminution and segregation of the feedstock, fresh feed mixture storage tanks, a horizontally mounted reactor with a cylindrical retort arranged horizontally, having a screw feeder and at one end is connected to the reservoir for the fresh mixture and merges at the other end in a vertically arranged sealed container for receiving the solid reaction product.
  • a burner and a fan are arranged in the horizontally mounted reactor.
  • the horizontal retort has openings for the exit of the gaseous mixture formed during the heating to the upper part of the combustion chamber of the reactor over its entire length. This gas mixture is burned with a deficiency of air.
  • the fuel gas leaving the reactor and the gas collecting in the vertically arranged retort may subsequently be used for industrial processes using scrubbing towers to purify the gases.
  • WO 2010/121574 A2 is a biomass energy recovery plant comprising a conveyor for transporting the biomass in a drying plant, which is connected to a reactor.
  • the system has a closed ORC circuit with several heat exchangers, wherein in the ORC circuit a turbine drives a generator and a connection point provides the generated electrical energy to customers. In addition, heat is provided to customers.
  • the plant makes progress in terms of energy recovery from biomass. However, it is only designed for biomass and for the energetic and material recovery of other combustible materials not suitable. In this respect, the field of application of this invention is considerably limited.
  • the object of the invention is therefore to provide a plant and a method for energy recovery from biomass and combustible waste as well as their recycling, which allow higher energy efficiency in continuous operation.
  • connection between the drying plant and the reactor is made by a arranged on the drying plant vertical conduit having a metering chamber in its lower part.
  • a further embodiment provides that the steam generator is arranged within the drying plant as a tube evaporator and is helical.
  • the condensate from the turbine receiving heat exchanger has a connection point for the supply of obtained heat energy in the public heating network, for the use of heat energy for cooling purposes and / or for drying purposes.
  • condensate from the turbine receiving heat exchanger is connected by means of a connection with a drying device which dries the biomass using the heat energy accumulating in this heat exchanger.
  • Particularly preferred embodiments of the invention provide to arrange the devices and facilities of the system in a compact biomass hall and a machine hall, which directly connects a partition, or to provide the compact system in the form of a portable container design.
  • An embodiment of the method provides that the biomass and the combustible wastes are comminuted to one to 15 mm x 15 mm x 40 mm.
  • the autothermal carbonization is initiated depending on the type of biomass and the combustible waste only after the stabilization of the temperature in the reactor and the exhaust gases between 650 ° C and 850 ° C.
  • the dried biomass and the waste are introduced at a temperature between 80 ° C and 100 ° C in the reactor.
  • biomass and the waste are dried for a residence time of 0.5 minutes to 3 minutes in a drying plant and carbonated in the reactor at a residence time of 3.4 seconds on average.
  • the Karbonmaschines is cooled to a temperature ⁇ 50 ° C, preferably ⁇ 40 ° C.
  • a particularly preferred embodiment of the method according to the invention comprises the biomass renewable raw materials, biological waste from the food industry and the industrial processing of fruits and vegetables, sorted municipal waste, wastewater treatment plants, animal biomass, bone meal and all other solid biological alternatives and waste.
  • the particular advantage of the system according to the invention and the method according to the invention is that of biomass and combustible waste of various kinds in an autothermal and continuous process without the use of Catalysts and water can be produced with high efficiency heat and electrical energy and biochar or alternatively, in addition to energy production as fertilizer or for soil improvement usable ashes can be produced.
  • the invention also allows a construction that requires only a small footprint. In a transportable variant, z.
  • the system can also be arranged on mobile platforms.
  • the inventive plant for energy recovery with integrated production of biochar and usable as fertilizer ashes consists of a biomass hall and an adjacent machine shop, both with a fixed, reproducible construction, fixed dimensions and the same color balance.
  • the biomass hall there are plants for the separation of the biomass, which are firmly connected with vertical and horizontal conveyors as well as plants for the shredding of biomass types of larger dimensions as well as screening plants.
  • the conveyors transport the biomass to the drying plant, which is connected to the reactor and at the output of the Karbonmaschineseck a cooling system is installed. Construction and operation of the reactor are in the patent PL 204 294 described.
  • the reactor is connected to a steam generator which operates a fixed turbine with a current generator and uses the waste heat energy generated during the carbonation. It also has piping connections, which make it possible to direct the resulting heat energy to the external consumers.
  • the reactor is equipped with a heating system operated by gas or oil, which initiates the ignition of the pyrolytic gases, with an air inlet opening, through which the air flows tangentially to the inner wall of the reactor, and with not less than two retorts.
  • the heating system of the reactor is used to initiate the autothermal process of carbonization of the biomass.
  • This system consists of an oil or gas burner with the requisite installation, a cylindrical metal combustion chamber with its cylindrical metal casing inside which the air blown in by a fan flows.
  • the air flowing through warms up in the chamber, the cylindrical metal panel forms.
  • the heated air mixes with the exhaust gases of the oil or gas burner, passes tangentially to the inner wall of the reactor and causes the hot air mixture in a circulation movement.
  • the mixture flows around the retorts and the inner ceramic wall of the reactor and simultaneously moves to the rear of the reactor.
  • the reactor is in the form of a cylindrical ceramic tunnel, which acts as a thermal battery for the autothermal process of combustion of the pyrolytic gases and ensures autothermal carbonization of the biomass.
  • the cylindrical ceramic tunnel stands on a firm foundation or is fixedly mounted on a movable platform. Its round walls are surrounded from the outside with a thermal insulation and with any solid housing, preferably made of sheet steel, clad. As thermal insulation is suitable for the needs of the invention insulating wool.
  • each retort Inside the reactor, no less than two single-sided closed retorts are fixed along its longitudinal axis. Their cross-sectional shape depends on the installed in them conveyor of charring biomass.
  • an arbitrary conveying device In the interior of each retort, an arbitrary conveying device is arranged with a temporally arbitrarily adjustable displacement of the biomass to be charred in the retort.
  • the feed feeder and the retort should be made of heat-resistant steel.
  • Each retort is provided from above with a customized in their shape of the conveyor cover. Along the cover, conical through-holes are attached to the interior of the reactor, the diameter of which increases from the inside to the outside of the retort cover.
  • the diameter of these openings is closely related to the granulation of the biomass to be charred and is proportional to this granulation.
  • the retorts closed on one side are mounted on several bases, which are attached to the ceramic bottom of the reactor. The height of these bases depends on the number of retorts mounted inside the reactor. This is adjusted so that the sum of the longitudinal axes of the retorts coincides with the length of the central axis of the inner reactor cylinder.
  • the retorts are housed inside the reactor so that from the side of the top metering of the biomass into the retort, near the vertical wall which closes the cylindrical ceramic reactor tunnel, an initial part of the device is housed, the biomass to be carbonized the retorts supplies.
  • the retorts are mounted in the front front wall of the reactor and protrude partially out of this wall for a length which ensures that the carbonation product can be completely disposed of therefrom.
  • the end pieces of the retorts form fixed drives of the conveyor which transport the biomass and the carbonization products inside each retort.
  • the biomass and carbonation products are moved inside each retort in countercurrent to the movement of the circulating air and the pyrolytic gases burning in the reactor.
  • a drying plant for the biomass to be carbonized is firmly mounted together with a steam generator.
  • the drying plant is inclined in the conveying direction of the biomass to be transported and dried to the rear wall of the reactor.
  • the angle of inclination should preferably not be less than 7 degrees.
  • the biomass drying plant is equipped in its front upper part, in front of its dense front wall, with a hopper for biomass to be dried.
  • the rear lower part of the drying plant is fixed to the reactor through a dense funnel tube through which the biomass is poured onto the conveyor mounted in the retorts.
  • the drying plant forms a rotatable metal tube, on the inner wall of a screw belt is fixed, whose stroke is equal to the inner diameter of the tube.
  • the screw conveyor fixedly arranged in the drying plant for the biomass to be dried is preferably a screw conveyor which conveys along the rotary tube of the drying plant.
  • the front part of the rotary tube is fixedly arranged in a rotary bearing, preferably a ring-spherical bearing, which in turn is mounted in the front wall of the drying plant.
  • the drive of this system preferably a chain drive is provided.
  • the rear part of the rotary tube is firmly housed in a swivel bearing, which is mounted in the rear wall of the drying plant.
  • the swivel bearing allows both the longitudinal and rotational displacement of the metal tube of the drying plant. The rotations of the drying plant are adjusted so that the biomass to be dried counter to the direction of flow the exhaust gases moved.
  • the residence time of the biomass in the drying plant depends on its moisture content.
  • the rotary screw conveyor of the drying plant extends in its lower part in a filling chamber made of heat-resistant steel with a vertically arranged conduit of any diameter for the dried biomass.
  • the filling chamber is attached both to the housing of the drying plant and to the vertical conduit for the dried biomass.
  • the dried biomass to be carbonated passes through cut-outs in the rotary kiln of the drying plant into the vertical pipe.
  • the vertical pipe is completed with a suitably shaped metering chamber made of heat-resistant material.
  • the front parts of the reactor cores are mounted with filling openings, thanks to which the dried biomass can be conveyed to the screw conveyors of each retort.
  • the metering chamber continuously meters the dried biomass to the respective retorts mounted inside the reactor.
  • the drying plant is connected to a steam generator, which forms a helical high pressure and high temperature resistant pipe.
  • the tube evaporator generates a high pressure steam.
  • the water flows through the helical tube in co-current with the exhaust gases of the reactor.
  • the generated high-pressure steam passes to the steam pipeline, through which it is routed via vent and shut-off valves for further use.
  • the high pressure steam feeds the turbine of a power generator via a discharge port with safety valve.
  • a dense condenser is provided for the hot product.
  • the cooler is connected at the front with a hopper to the screw conveyor of the reactor. It cools the hot Karbonleiterseck with water, preferably according to the countercurrent principle.
  • the cooler for the Karbonmaschineseck has a cylindrical chamber, preferably a double-walled tube through which the production water flows between the inner and outer wall in the opposite direction to the funded hot Karbonmaschineseck.
  • the cooler for the carbonation product comprises a rotary screw conveyor. It is cooled along its length with the countercurrent flowing water. Inside the cylindrical chamber of the cooler, which is surrounded by an outer wall, the screw of the conveyor is arranged inside the cylindrical chamber of the cooler, which is surrounded by an outer wall, the screw of the conveyor is arranged. The outer wall of the cylindrical chamber of the radiator forms a metal outer shell.
  • the inner wall of the double-walled tube forms the housing for the chamber of the screw conveyor.
  • at its front part of the screw conveyor has a fixed mounted electric motor with gear, preferably also with an inverter.
  • the chamber of the cooler is fixedly connected to the lower part of the hopper for the hot Karbonleiterseck that comes to the screw conveyor of the cooler.
  • the chamber of the screw conveyor is cooled with production water flowing in the cylindrical space formed by the housing of the screw conveyor and the metal outer shell. The water flows in the opposite direction to the conveyed by the screw conveyor Karbonmaschines employments.
  • the housing of the chamber of the conveyor and the outer jacket and the lateral covers of the cylindrical space of the double-walled radiator tube are made of temperature and pressure resistant boiler materials.
  • the preferably cooled to a temperature of less than 40 ° C carbonation product is passed through a filler pipe to another fixed mounted conveyor of any kind.
  • a Telleraufgeber equipped with a chamber in which a loosening of the product takes place. It is advantageous that this chamber is filled with CO 2 to extinguish any sparks.
  • the chilled and extinguished product is a high-quality fuel which is then transported to a packing device and assembled into big-bag containers.
  • a blower pushes air into the heating system, where the mixing of the air with the hot exhaust gases of the oil or gas burner takes place.
  • the mixing takes place only during heating.
  • the shutdown of the oil or gas burner and the closure of the inflow of hot exhaust gases takes place in the Auffilstrom.
  • the exhaust gases not completely combusted in the reactor flow through a vertical opening in the rear part of the drying plant tangentially to its cylindrical inner wall. In this room, if necessary, secondary air is forced in to leave the reactor Completely burn exhaust gases.
  • the resulting at the end of the combustion process hot exhaust gases flow in a swirling motion to the front of the dryer. They heat the rotary kiln of the drying plant for the biomass and thereby dry the biomass located in its interior, moving in the opposite direction to the flow of combustion gases and to be carbonated. After that, the exhaust gases pass through the existing in the front part of the drying system opening to the exchanger water / exhaust gases and then they are passed through a blower via the exhaust pipe for cleaning and then to the chimney.
  • the plant according to the invention has three production water systems.
  • a circulating water pump under the pressure of 2.0 MPa, pushes the water into the line to the water / waste water exchanger, where the heating takes place.
  • the water flows to the installed in the interior of the exhaust gas cooler steam generator in / or the reduction turbine with the current generator.
  • the condensate then becomes the exchanger hot water / water and then to the tube exchanger, where the lack of water is supplemented with raw water.
  • the supplementary pump draws the cooled production water and the raw water back into the feedwater installation via the circulation pump.
  • cold water is sent to the exchanger via the feed water line.
  • a tube exchanger is installed, which heats the water with the hot water from the first system.
  • the thus heated water is intended for social purposes of operation: central heating and hot water boiler.
  • Another separate system is the installation for cooling the biochar.
  • Cold water from the feed water pipe is directed to the conveyor of the product - the biochar - and enters the space between the inner and outer walls of the cylindrical chamber of the product cooler. After leaving the cooler at the temperature of 70 ° C, the water is used to irrigate the product - the biochar.
  • the energy recovery operation is a thermolysis plant that continuously produces some of its products: a refined solid fuel with controlled calorific value and / or renewable electrical energy and / or thermal energy and / or hot waste gases from different sources: solid biodegradable remains of the food industry and industrial processing of fruit and vegetables, sorted municipal waste, municipal wastewater treatment waste, animal biomass, including meat bone meal, plant biomass, among them also from plantations of energy crops and from all other solid biodegradable alternative and waste fuels.
  • the preparation of the waste fuels by processing in the thermolysis operation for energy recovery consists in a crushing into grains, the size of which should not exceed the dimensions 15x15x40 mm. A prepared fuel is transported mechanically into the hopper of the rotary drying unit.
  • the dry screw auger mounted in the lower part of the hopper transports the waste fuel along the cylindrical metal chamber which forms a helical tube and through which the exhaust gases leaving the reactor move in a direction opposite to the moving waste fuel.
  • the biomass remains in the drying plant for 0.5 minutes to 2 minutes.
  • the dried biomass heated up to the temperature of approx. 90 ° C is directed via a vertical tube to the conveyor of the reactor cores.
  • On the opposite side of the filling line of the retort conveyor is introduced through the tangential to the inner wall of the reactor chamber mounted opening the air with which the exhaust gases are burned, which escape from the reactor during an oxygen-free charring of the waste fuel.
  • the flame of the burning gases forms an elongated vortex ring in the retorts, inside which are the waste to be processed and moving.
  • the required technical parameters of the fuel to be produced in the thermolysis module of the energy recovery are achieved by setting a corresponding rotational speed of the screw conveyor inside each retort.
  • the time required to produce the product for the flow of waste fuel depends on the temperature of the charring process in the reactor and on the type of biomass.
  • the temperature of 200 ° C to 370 ° C having hot fuel with given technical parameters is transported from the reactor with the screw conveyor, which is also the cooling system for the final product.
  • the cooling system reduces the temperature of the product to less than 40 ° C.
  • the chill conveyor of the cooling system transports the cooled fuel with given technical parameters to the container for the product, which is an integral part of the energy recovery thermolysis module.
  • the product In the screw conveyor, the product is cooled with the production water flowing in the space between the tube walls along the conveyor in the opposite direction to the product transported by the conveyor.
  • the by-products of the process of fuel production in the thermolysis module of energy recovery are: hot production water, hot water vapor and exhaust gases depending on the processed fuel type. The exhaust gases produced in the process are released to the atmosphere after cleaning.
  • thermolysis module of the energy recovery is the possibility of processing any biodegradable municipal waste and / or industrial waste and / or vegetable biomass and / or animal biomass to the full-value product with over 65% content of carbon C and high Nutzparametem whose Value can be adjusted as required, depending on the individual requirements of the customer of the product.
  • Another advantage is the high efficiency of the thermolysis module resulting from the continuity of the manufacturing process as well as from the existing countercurrent drying and thermolysis process. Benefits also include full utilization of the thermal energy generated in the thermolysis module as a result of the production process of full-fledged fuels and the energy of the waste products of the combustion process.
  • the Thermolyse-Bertieb produces the "green” electric energy and renewable heat energy for energy recovery.
  • thermolysis operation for energy recovery is established from the viewpoint of utilizing substantial quantities of biodegradable waste fuels, there is the possibility of producing the "green” electric power of particular power as well as a renewable heat energy of proportional power and / or refrigeration of local industrial importance.
  • a significant advantage of this invention is also the fact that the product - the biochar - can possess parameters that make it both a renewable fuel for power and district heating, as well as a fuel for coal fuel cells, as well as a natural fertilizer long-term decay cycle without emission of C0 2 qualify.
  • the process of carbonization of plant biomass begins with the stabilization of the temperature at 650 ° C. This is achieved by the swirling of the flame, which completely burns the pyrolytic gases in the reactor and stabilizes the temperature of the exhaust gases escaping from the reactor.
  • Crushed vegetable biomass (grains smaller than 40 mm) with the parameters: humidity below 40% ash up to 2% calorific value over 9.0 MJ / kg is continuously transported with a belt conveyor in the hopper of the biomass drying plant, which is located inside the exhaust gas cooler.
  • the residence time of the plant biomass in the drying plant is regulated depending on its moisture content and lasts up to 90 seconds.
  • the plant biomass After the plant biomass has left the drying plant at a temperature of up to 90 ° C, it is directed through a metal filling chamber to the screw conveyors of the reactor cores.
  • the dried vegetable biomass is subject to the thermolysis process at a temperature of over 650 ° C in the reactor.
  • the residence time in the reactor is 3.5 seconds on average.
  • the fuel produced by the thermolysis process After passage through the reactor, the fuel produced by the thermolysis process, at a temperature below 370 ° C, is passed into a sealed container for the hot product. From here it passes through a water cooled screw conveyor into the cooler of the product.
  • the biochar thus produced cooled to a temperature below 40 ° C., is completely extinguished with CO 2 for safety reasons, moistened with water (to preferably below 10% moisture) and conveyed by a conveyor to the packing device of the Transported biochar, in which this is made up.
  • a "green” fuel the biochar
  • the biomass of the plant with simultaneous energy recovery from the renewable raw materials, with the following parameters: absolute humidity below 10% ash content below 6.0% absolute carbon content over 70% sulfur content approx. 0.01% chlorine content approx. 0.01% calorific value over 24MJ / kg
  • the carbonization of hard-deciduous plant biomass begins with the stabilization of the temperature of 650 ° C. This is achieved by the swirling of the flame, which completely burns the pyrolytic gases in the reactor and stabilizes the temperature of the exhaust gases escaping from the reactor.
  • the comminuted vegetable biomass (grains smaller than 20 mm) with parameters: humidity below 40% ash up to 0.5% calorific value over 10.0 MJ / kg is continuously transported with a belt conveyor in the hopper of the biomass drying plant, which is located inside the exhaust gas cooler.
  • the residence time of the plant biomass in the drying plant is also regulated in this case depending on its moisture content and is up to 90 seconds.
  • the dried ones Vegetable biomass is subject to the thermolysis process at a temperature of over 700 ° C in the reactor.
  • the residence time in the reactor is 3.5 seconds on average.
  • thermolysis light hydrocarbons are released from the vegetable biomass.
  • the fuel produced by the thermolysis process is passed at a temperature below 370 ° C to a sealed container for the hot product. From here it passes through a water cooled screw conveyor into a cooler.
  • the biochar generated, cooled to a temperature of less than 40 ° C, is completely quenched with CO 2 for safety reasons and moistened with water (preferably to a moisture content of less than 6%). Finally, it is transported by a conveyor to the device for packaging the biochar.
  • the carbonization process of solid biomass consisting of combustible plastics, biomass municipal waste and plant biomass, begins with the stabilization of the temperature of 850 ° C. This is achieved by the swirling of the flame, which completely burns the pyrolytic gases in the reactor and stabilizes the temperature of the exhaust gases escaping from the reactor.
  • the solid and thoroughly mixed biomass in crushed form is used with the following parameters: humidity below 40% plastics below 3.5% Biomass municipal waste below 35% vegetable biomass over 55%
  • the waste biomass is conveyed continuously with a belt conveyor into the hopper of the drying plant, which is arranged inside the exhaust gas cooler.
  • the residence time of the waste biomass in the drying plant is regulated depending on its moisture content and lasts up to 90 seconds. After the waste biomass with a temperature of up to 90 ° C has left the drying plant, it is transported through a metal filling chamber to the conveyor cores of the reactor cores.
  • the dried waste biomass is subject to the thermolysis process in the reactor at a temperature of more than 850 ° C.
  • the residence time in the reactor is 3.5 seconds on average. During the thermolysis, light hydrocarbons as well as sulfur and chlorine oxides are liberated from the plant biomass.
  • the fuel produced by the thermolysis process at a temperature of less than 370 ° C is passed into a sealed container for the hot product. From here it passes through a water cooled screw conveyor into the cooler of the product.
  • the generated fuel, cooled to a temperature of less than 40 ° C, is completely extinguished with CO 2 for safety reasons and moistened with water (preferably to a moisture content of less than 6%) and transported by a feeder system to the container of the finished product.
  • a fuel for heating purposes is produced from solid biomass waste fuels with the following parameters: humidity ⁇ 10% ash content ⁇ 25% absolute carbon content > 65% sulfur content approx. 0.2% chlorine content approx. 0.3% calorific value > 21MJ / kg.
  • Fig. 1 shows that the plant consists of a hall 2 for the biomass and a machine hall 4, which are interconnected by means of a partition wall 3 and at the same time for the biomass 1 receives a screening plant 5, which in turn is connected to the conveyor 6.
  • the drying unit 7 is connected, which is designed in the present example as a rotary drying system.
  • the drying plant 7 is firmly connected to the reactor 8.
  • the cooler 9 for the finished reaction product, the biochar 14, is arranged.
  • the radiator 9 is followed by the conveying device 10 and to it the CO 2 extinguishing device 11 and the moistening device 12 as well as a packing device 13 for the packaging of the cooled product 14, the biochar.
  • the system according to the invention is equipped with a production water system 15 operating in a closed circulation system.
  • This system comprises the heat exchanger 16 water / exhaust gases for cooling / heat transfer of the exhaust gases of the rotary drying plant 7.
  • the heat exchanger 16 is fixedly connected to the steam generator 17 and this in turn with the turbine 18.
  • the turbine 18 operates the current generator 19.
  • the "green” electrical energy generated by the current generator 19 is introduced via the connection point 20 into the power grid 21.
  • the turbine 18 is connected to the exchanger 22 condensate / water.
  • the "green" heat energy thus obtained is made available to the consumers 23 and may alternatively be fed into the public heating network 23a of the respective location, used for refrigeration 23b and / or with the connection 23c for drying the biomass 1 to be processed.
  • the partially cooled production water coming from the exchanger 22 flows through the exchanger 40 water / water and transfers the existing heat energy to the raw water supplied via the connection 37.
  • the water thus heated may be supplied through the connection 39 for the social purposes of the enterprise, e.g. a hot water boiler and can be used in the colder months for heating purposes.
  • the raw water supplied via the connection 37 is used for cooling the finished reaction product, the biomass 14, in the exchanger 9, and then for moistening the biomass 14 in the moistening device 12.
  • the plant according to the invention further includes the permanently connected to the reactor 8 oil or gas installation 24, with the help of the commissioning of the technological process injected, so it is given the first impetus.
  • the port 24 is connected to the fan 25 for supplying the combustion air required for heating for the oil or gas installation 24.
  • the reactor 8 is connected to the forwarding of its hot exhaust gases by means of the pipe 26 to the rotary dryer 7 and the steam generator 17, in which the hot exhaust gases are cooled by the energy consumed in the steam generation something.
  • the steam generator 17 is connected by means of the exhaust pipe 27 with the heat exchanger 16 exhaust gases / water. From there, the cooled exhaust gases pass through the piping system 27a first to the filter device 28, preferably a pocket filter, then to Exhaust fan 29 and finally to the chimney 30 through which they enter as purified and cooled exhaust gases in the free atmosphere.
  • the plant according to the invention is characterized in particular by the fact that the process of recovering the energy contained in the biomass 1 and the combustible wastes is designed as an autothermal process in which the biomass 1 and the waste are, so to speak, their own energy sources.
  • oil or gas is an automatic supply of biomass 1 or waste from the biomass hall 2 to the screen 5 and by means of the conveyor 6 to the rotary drying unit 7 and then to the reactor. 8
  • the process of thermal upgrading of the biomass 1 takes place according to the in the Polish patent PL 204 294 described method.
  • Biomass 1's thermal upgrading is understood as meaning both carbonization of biomass 1 and its upgrading to a solid "green” (FLUID) fuel, biochar 14, as well as the recovery of "green” energy.
  • FLUID solid "green”
  • Biochar 14 As well as the recovery of "green” energy.
  • In the process of carbonization excessive heat energy is generated, which is transported by the hot exhaust gases of the reactor 8 to the rotary drying plant 7. From there they flow around the steam generator 17 and finally reach the heat exchanger 16 exhaust gases / water, in which further heat energy is transferred to the water flowing to the steam generator 17.
  • the cooled to a temperature of ⁇ 120 ° C exhaust gases flow through the exhaust pipe 27 a to the filter device 28 and are then passed by the exhaust fan 29 to the chimney 30, through which they are released as purified and cooled exhaust gases 31 into the atmosphere.
  • Fig. 2 shows the technological flow of the air used in the system according to the invention and the exhaust gases forming in the production process, starting with the air supplied by the blower 25 for the oil or
  • Fig. 3 shows the closed circulation system 15 of the required for the production process for the production of biochar 14 water and steam and two open water systems for use of the connection 37 supplied raw water once for cooling and spraying the Karbonmaschines organizations and the other for the use of heated feed water for economic / social purposes of the company via the connection 39.
  • the already heated by the hot exhaust gases from the rotary dryer 7 used here in the exchanger 16 water is evaporated in the evaporator 17 by flowing from the reactor 8 in the rotary drying system 7 very hot exhaust gases and drives the turbine 18 at.
  • the heat of the condensate flowing out of the turbine 18 is transferred in the exchanger 22 to corresponding consumers 23.
  • the exchanger 40 the production water is still heat energy available for use for economic / social purposes of the company before it is reheated in the exchanger 16 by the hot exhaust gases from the rotary dryer 7 and the cycle begins again. If necessary, the volume of the production water circulating in the closed system 15 can be kept at the required level by supplying raw water into the piping between the heat exchanger 40 and the heat exchanger 16.
  • Fig. 4 shows a schematic representation of the achievable by the thermal upgrading of the biomass 1 results.
  • Paragraph 20 indicates the production of green energy for the public electricity network
  • paragraph 14 documents the production of the green biochar
  • paragraphs 23a, 23b and / or 23c indicate the production of 'green' heat energy network and / or for cooling purposes 23b and / or for drying processes, such as for drying the still moist biomass.
  • Fig. 5 shows the scheme of a biomass recovery plant 1 with a high content of ash by carbonation with integrated production of a natural fertilizer for agricultural or horticultural purposes.
  • the present embodiment of the invention relates in particular to the carbonization of deposits from the treatment of municipal wastewater, to waste substrates from biogas plants, to waste from industrial agriculture, such as meat-bone meal, and to waste from the food industry, predominantly with a granulation 0, 1 mm to 5 mm, a moisture content ⁇ 95%, an ash content> 15% and a calorific value> 6 MJ / kg.
  • the process of carbonization with subsequent incineration of such as ash-containing biomass 1 begins with the stabilization of the temperature of 850 ° C, which expediently by a turbulence of the flame of the burning in the reactor 8 reached pyrolytic gases and thereby at the same time the temperature of the escaping from the reactor 8 exhaust gases is stabilized.
  • the ash-containing biomass 1 is predried using the heat energy 23c obtained in the process in a drying plant 38 provided in the biomass hall 2, which is preferably a plant according to the fluidized bed process.
  • the biomass hall 2 is firmly connected to the partition wall 3 to the machine hall 4 and the screen 5 with the conveyor 6.
  • the rotary drying system 7 is connected. It is connected to the reactor 8.
  • the resulting in the reactor 8 by the carbonization hot char 14 is promoted by means of the fixed to the reactor 8 screw conveyor 32 to the ashing device 33 and then to the cooler 9 of the Karbonmaschines inhabits, the ashes.
  • the hot ashing product is cooled by means of the supply 37 via the raw water.
  • the conveyor 10 is arranged, with which the cooled product is conveyed to the packing device 13, which assembles it for shipping.
  • the ashes obtained in this way can be used in agriculture as well as in garden centers for soil improvement and as a natural fertilizer.
  • a production water installation 15 which operates in a closed circulation system, and two open water systems for the supplied via the port 37 raw water.
  • the first open system is a heat exchange for heating the raw water supplied through the port 37 to the social use exchanger 40.
  • the other open system is to use the supplied raw water to cool the product in the exchanger 9.
  • This system is connected to the installation of the production water in front of the entrance to the exchanger 16 water / exhaust gases.
  • the circulation system of the production water includes the fixed-mounted exchanger 16 water / exhaust gases for transmitting the heat flowing from the rotary dryer 7 still hot exhaust gases.
  • the exchanger 16 is fixed to the exchanger 35 and this connected to the evaporator 17, whose high-pressure steam drives the turbogenerator 36 and which is connected to means 20 for feeding the "green" electrical energy into the power grid 21.
  • the hot water flowing out of the exchanger 16 is further heated by the heat produced during complete carbonization in the ashing device 33.
  • the turbogenerator 36 is fixedly connected to the exchanger 22 - condensate / water - which is connected by means of the terminal 23 c to the customer of the renewable heat energy, the plant 38 for the predrying of waste biomass 1.
  • Part of this embodiment of the system according to the invention is also an oil or gas installation 24 permanently connected to the reactor 8, which gives the technology process the initial ignition.
  • the installation 24 has the air blower 25.
  • a channel 26 is also mounted for the hot exhaust gases in this embodiment, which are fed by means of this channel of the rotary dryer 7.
  • the slightly cooled in the evaporator 17 from the reactor 8 flowing exhaust gases pass through the exhaust pipe 27 to the exchanger 16 - exhaust gases / water.
  • the exhaust gases from the ashing device 33 and the exchanger 35 are also passed to the evaporator 17 in which they give this heat energy for steam generation. Thereafter, they are passed to the exchanger 16 - exhaust gases / water.
  • this technological process of energy recovery with integrated production of natural fertilizer is characterized by the fact that the biomass 1 used in this process is also the carrier of the autothermal process of energy recovery.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Inorganic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Processing Of Solid Wastes (AREA)
  • Fertilizers (AREA)

Claims (15)

  1. Installation pour la récupération d'énergie à partir d'une biomasse et de déchets combustibles et pour la carbonisation de ces substances, comprenant un dispositif de séparation, broyage et/ou tamisage (5) relié à une installation de transport (6) pour le transport de la biomasse dans une installation de séchage (7), un réacteur (8) relié à l'installation de séchage (7), au niveau duquel une installation de gaz ou de mazout (24) avec une soufflante (25) est disposée, ainsi que des échangeurs de chaleur et dispositifs pour refroidir et nettoyer des gaz d'échappement,
    caractérisée en ce que
    a) le réacteur (8) est relié à un refroidisseur (9) qui recueille le produit de la carbonisation provenant du réacteur (8) et qui est relié à un dispositif de transport (10) qui transporte le produit de carbonisation vers un dispositif d'extinction (11), ensuite vers un dispositif d'humidification (12), et finalement vers un dispositif de conditionnement (13) qui conditionne le produit, un biocharbon (14),
    ou
    b) le réacteur (8) est relié à un dispositif de transport (32) qui transporte le produit de carbonisation produit par la carbonisation dans le réacteur (8) vers un dispositif d'incinération (33), et le dispositif d'incinération (33) est relié à un refroidisseur (9), et celui-ci à un dispositif de transport (10) qui transporte le produit d'incinération vers un dispositif de conditionnement (13) qui le conditionne dans des contenants adéquats,
    et l'installation présente, pour les besoins de la récupération d'énergie,
    en a) un système de circulation d'eau de production (15) fermé, comprenant
    - un échangeur de chaleur (16) pour refroidir les gaz d'échappement chauds, amenés au moyen d'une conduite (27), de l'installation de séchage (7), et le transfert de chaleur simultané à l'eau de production amenée de l'échangeur de chaleur (16) vers un évaporateur (17), l'évaporateur (17) étant entouré par le flux des gaz d'échappement chauds amenés via une conduite (16) hors du réacteur (8) et est relié à une turbine (18), laquelle entraîne un générateur (19), et un point de connexion (20) qui met à disposition de consommateurs (21) l'énergie électrique produite ;
    - un échangeur de chaleur (22) pour transmettre la chaleur du condensat chaud amené hors de la turbine (18) à l'eau amenée via un système ouvert pour l'exploitation économique ultérieure de l'eau chauffée au consommateur (21) ;
    - un échangeur de chaleur (40) relié à l'échangeur de chaleur (16) pour la transmission de la chaleur résiduelle de l'eau de production amenée hors de l'échangeur de chaleur (22) à l'eau brute amenée via le système ouvert avec un raccordement (37), laquelle est à disposition de manière chauffée au moyen d'un raccordement (39) pour des consommateurs pour une utilisation ultérieure ;
    et
    en b) un système de circulation d'eau de production (15) fermé, comprenant
    - un échangeur de chaleur (16) pour refroidir les gaz d'échappement chauds, amenés au moyen d'une conduite (27), de l'installation de séchage (7), dans laquelle cet échangeur de chaleur (16) est relié à un échangeur de chaleur (35) pour la transmission de la chaleur des gaz d'échappement chauds produits dans le dispositif d'incinération (33) à l'eau de production amenée de l'échangeur de chaleur (16) vers l'échangeur de chaleur (35), et l'échangeur de chaleur (35) est relié à un évaporateur (17), l'évaporateur (17) étant entouré par le flux des gaz d'échappement chauds, amenés au moyen d'une conduite (26), du réacteur (8) et est relié à une turbine (18), laquelle entraîne un générateur (19), et un point de connexion (20) qui met à disposition de consommateurs (21) l'énergie électrique produite ;
    - un échangeur de chaleur (22) pour la transmission de la chaleur du condensat chaud amené hors de la turbine (18) à l'eau amenée via un système ouvert pour l'exploitation économique ultérieure de l'eau chauffée au consommateur (21) ;
    - le refroidisseur (9) faisant office d'échangeur de chaleur pour la transmission de la chaleur du produit d'incinération chaud à l'eau brute amenée via un raccordement (37), le refroidisseur (9) est relié à une conduite, menant d'un échangeur de chaleur (40) vers l'échangeur de chaleur (16), devant l'entrée de celle-ci dans l'échangeur de chaleur (16) ;
    - l'échangeur de chaleur (40) relié à l'échangeur de chaleur (16) pour la transmission de la chaleur résiduelle de l'eau de production amenée hors de l'échangeur de chaleur (22) à l'eau brute amenée via un système ouvert avec un raccordement (37), laquelle est disponible pour des consommateurs de manière chauffée au moyen d'un raccordement (39) pour une utilisation ultérieure.
  2. Installation selon la revendication 1, caractérisée en ce que la liaison entre l'installation de séchage (7) et le réacteur (8) est établie grâce à un conduit vertical disposé au niveau de l'installation de séchage (7), lequel présente une chambre de dosage dans sa partie inférieure.
  3. Installation selon la revendication 1 ou 2, caractérisée en ce que le générateur de vapeur (17) est réalisé en tant qu'évaporateur tubulaire à l'intérieur de l'installation de chauffage (7) et est formé de manière hélicoïdale.
  4. Installation selon l'une des revendications 1 à 3, caractérisée en ce que l'on prévoit, au niveau de l'échangeur de chaleur (22), un point de raccordement (23a) pour alimenter le réseau de chauffage public avec l'énergie thermique obtenue, un point de raccordement (23b) pour des besoins de refroidissement et/ou un point de raccordement (23c) pour des besoins de séchage.
  5. Installation selon l'une des revendications 1 à 4, caractérisée en ce que l'échangeur de chaleur (22) est relié au moyen d'un raccordement à un dispositif de séchage (38), lequel assure le pré-séchage de la biomasse (1) en utilisant l'énergie thermique produite dans l'échangeur de chaleur (22).
  6. Installation selon l'une des revendications 1 à 5, caractérisée en ce que les dispositifs et équipements de l'installation sont disposés dans un hall à biomasse (2) et dans un hall des machines (4) respectivement réalisés de manière compacte, lesquels sont directement reliés ensemble par une cloison (3).
  7. Installation selon la revendication 6, caractérisée en ce que la réalisation compacte de l'installation est une réalisation transportable de conteneur.
  8. Installation selon l'une des revendications 5 à 7, caractérisée en ce que la biomasse (1) comprend des matières premières renouvelables, des déchets biologiques de l'industrie alimentaire et de la transformation industrielle de fruits et légumes, des déchets municipaux triés, des dépôts de stations d'épuration, de la biomasse animale, de la poudre d'os ainsi que toutes les autres matières biologiques solides alternatives et de rebut.
  9. Procédé pour la récupération d'énergie et la carbonisation de biomasse et de déchets combustibles, caractérisé en ce que la biomasse et les déchets sont amenés en continu de manière broyée et séchée à un réacteur chauffé et, après la stabilisation de la température nécessaire pour la carbonisation et après la stabilisation de la température des gaz d'échappement du réacteur, sont soumis à houillification dans celui-ci, sans oxygène et de façon autothermique, et les gaz d'échappement ainsi produits sont refroidis et nettoyés et le produit de houillification chaud est soit
    a) refroidi et, après un traitement avec du CO2 ayant eu lieu pour des raisons de sécurité, est humecté avec de l'eau et est finalement conditionné dans un dispositif de conditionnement en tant que biocharbon,
    soit
    b) amené à un dispositif d'incinération, est complètement brûlé dans celui-ci, la cendre ainsi formée est ensuite refroidie et est ensuite amenée à un dispositif de conditionnement dans lequel la cendre est conditionnée pour des besoins de fertilisation ou des besoins d'amélioration des sols pour des consommateurs,
    et pour les besoins de la récupération d'énergie
    en a)
    - les gaz d'échappement chauds issus du réacteur sont utilisés à contre-courant pour le séchage de la biomasse et des déchets broyés prévus pour la carbonisation et sont ensuite guidés à travers un échangeur de chaleur et, dans celui-ci, continuent de chauffer l'eau guidée dans un système de circulation d'eau de production fermé, celle-ci étant amenée à un générateur de vapeur et étant transformée dans celui-ci en vapeur sous haute pression, par les gaz d'échappement chauds du réacteur, avec laquelle une turbine d'un générateur est entraînée pour la génération d'énergie électrique, et l'énergie électrique générée est mise à disposition de consommateurs,
    - l'énergie thermique du condensat chaud s'écoulant hors de la turbine est transmise au moyen d'un échangeur de chaleur à l'eau amenée via un système externe et est mise à disposition de consommateurs pour des besoins de chauffage, de séchage et de refroidissement, et
    - la chaleur résiduelle de l'eau de production s'écoulant hors de l'échangeur de chaleur cité en dernier est transmise par un autre échangeur de chaleur à de l'eau brute amenée et mise à disposition de l'entreprise dans laquelle l'installation selon l'invention est installée pour des besoins sociaux ;
    et en b)
    - les gaz d'échappement chauds issus du réacteur pour le séchage de la biomasse et des déchets broyés prévus pour la carbonisation sont utilisés à contre-courant et sont ensuite guidés à travers l'échangeur de chaleur (16) et, dans celui-ci, l'eau amenée dans un système de circulation d'eau de production fermé continue d'être chauffée avant qu'elle n'absorbe, dans un autre échangeur de chaleur, l'énergie thermique des gaz d'échappement chauds s'écoulant hors d'un dispositif d'incinération, et l'eau de production ainsi chauffée est amenée à un générateur de vapeur et est transformée dans celui-ci en vapeur sous haute pression, par les gaz d'échappement chauds du réacteur, avec une turbine d'un générateur est entraînée et l'énergie électrique ainsi générée est mise à disposition de consommateurs ;
    - l'énergie thermique du condensat chaud s'écoulant hors de la turbine est transmise au moyen d'un échangeur de chaleur à l'eau amenée via un système externe et est mise à disposition de consommateurs pour des besoins de chauffage, de séchage et de refroidissement, et
    - la chaleur résiduelle de l'eau de production s'écoulant hors de ce dernier échangeur de chaleur est transmise par un autre échangeur de chaleur à de l'eau brute amenée et est mise à disposition de l'entreprise dans laquelle l'installation selon l'invention est installée pour des besoins sociaux.
  10. Procédé selon la revendication 9, caractérisé en ce que la biomasse et les déchets combustibles sont broyés à un jusqu'à 15 mm x 15 mm x 40 mm.
  11. Procédé selon la revendication 9 ou 10, caractérisé en ce que la carbonisation autothermique est initiée en fonction du type de la biomasse et des déchets combustibles avec stabilisation de la température dans le réacteur et celle des gaz d'échappement entre 650 °C et 850 °C.
  12. Procédé selon l'une des revendications 9 à 11, caractérisé en ce que la biomasse séchée et les déchets sont introduits dans le réacteur avec une température comprise entre 80 °C et 100 °C.
  13. Procédé selon les revendications 9 à 12, caractérisé en ce que la biomasse et les déchets sont séchés dans une installation de séchage avec durée de séjour de 0,5 minutes à 3 minutes.
  14. Procédé selon l'une des revendications 9 à 13, caractérisé en ce que la biomasse et les déchets sont carbonisés dans le réacteur avec une durée de séjour de 3,4 secondes en moyenne dans le réacteur.
  15. Procédé selon l'une des revendications 9 à 14, caractérisé en ce que le produit de carbonisation est refroidi jusqu'à une température < 40 °C.
EP11709323.7A 2011-01-13 2011-01-28 Procédé et installation permettant la récupération d'énergie à partir de la biomasse et des déchets combustibles, en particulier des matières premières renouvelables, ainsi que leur carbonisation Not-in-force EP2663742B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE202011001453U DE202011001453U1 (de) 2011-01-13 2011-01-13 Anlage zur Energierückgewinnung aus Biomasse und brennbaren Abfällen, insbesondere nachwachsenden Rohstoffen sowie zur Karbonisierung
PCT/EP2011/000382 WO2012095119A2 (fr) 2011-01-13 2011-01-28 Procédé et installation permettant la récupération d'énergie à partir de la biomasse et des déchets combustibles, en particulier des matières premières renouvelables, ainsi que leur carbonisation

Publications (2)

Publication Number Publication Date
EP2663742A2 EP2663742A2 (fr) 2013-11-20
EP2663742B1 true EP2663742B1 (fr) 2018-06-27

Family

ID=43972876

Family Applications (1)

Application Number Title Priority Date Filing Date
EP11709323.7A Not-in-force EP2663742B1 (fr) 2011-01-13 2011-01-28 Procédé et installation permettant la récupération d'énergie à partir de la biomasse et des déchets combustibles, en particulier des matières premières renouvelables, ainsi que leur carbonisation

Country Status (3)

Country Link
EP (1) EP2663742B1 (fr)
DE (2) DE202011001453U1 (fr)
WO (1) WO2012095119A2 (fr)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012019564A1 (de) * 2011-10-08 2013-04-11 Wilke Engelbart Verfahren und Vorrichtung zur Herstellung von Dünger-Kohle
EP2657469A1 (fr) * 2012-04-25 2013-10-30 Burmeister & Wain Energy A/S Système de production d'énergie à combustible de biomasse
WO2014053083A1 (fr) * 2012-10-06 2014-04-10 Beijing Bht Environ Tech Co., Ltd Procédé et dispositif pour produire du charbon à base d'engrais se présentant sous une forme compactée
US10351455B2 (en) 2013-11-25 2019-07-16 University Of Idaho Biochar water treatment
CN106630530A (zh) * 2015-10-30 2017-05-10 新大陆科技集团有限公司 一种反应釜及应用其的富水生物质干化及能量回收系统
AT518570B1 (de) * 2016-04-25 2018-06-15 Ing Dr Techn August Raggam Dipl Vorrichtung zum Erzeugen von Holzkohle
CN111716607A (zh) * 2020-06-18 2020-09-29 芜湖浩博科技有限公司 一种冷却水管总成热烘成型生产线
CN112177696A (zh) * 2020-08-24 2021-01-05 东南大学 耦合垃圾处理与燃煤发电的系统及方法

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
PL102394B1 (pl) 1976-06-11 1979-03-31 A device for obtaining charcoals from fine lignocellulose waste material
PL112639B1 (en) 1978-01-14 1980-10-31 Inst Tele I Radiotech High frequency generator system for testing temperaturedependent frequency and resistance characteristics of quartz resonators
PL116022B2 (en) 1978-01-27 1981-05-30 Inst Chemii Przemyslowej Method of manufacturing fibre reinforced plastic products of improved stiffness
GR1001615B (el) * 1993-06-04 1994-07-29 Viokat Anonymos Techniki & Vio Μέ?οδος αεριοποίησης στερεών καυσίμων χαμηλού ?ερμικού περιεχομένου με ωφέλιμη αξιοποίηση στην παραγωγή ηλεκτρικής ενέργειας χωρίς δημιουργία ρύπανσης περιβάλλοντος.
DE4342165C1 (de) * 1993-12-10 1995-05-11 Umwelt & Energietech Verfahren zur energetischen Nutzung von Biomasse
FR2720479B1 (fr) 1994-05-30 1996-07-12 Inst Francais Du Petrole Procédé et installation de pyrolyse de déchets ayant une unité de préchauffage.
WO1999010682A1 (fr) * 1997-08-27 1999-03-04 Siemens Aktiengesellschaft Installation et procede pour l'elimination thermique des dechets
US6510695B1 (en) * 1999-06-21 2003-01-28 Ormat Industries Ltd. Method of and apparatus for producing power
DE20206016U1 (de) 2002-04-17 2002-11-21 Feuerecker, Josef, 94486 Osterhofen Reifenventilkappe und Ventilkappenbeilage mit Angabe der Radposition
DE102008004732A1 (de) 2008-01-16 2009-07-23 Lucia Viviane Sanders Hydrothermale Karbonisierung von Biomasse
DE102008028953A1 (de) 2008-06-18 2009-12-24 Hydrocarb Gmbh & Co. Kg Verfahren zur Erzeugung von Kohle aus Pflanzen und Pflanzenresten
DE102008056006B4 (de) 2008-11-05 2023-07-06 Grenol Ip Gmbh Verfahren und Vorrichtung zur hydrothermalen Karbonisierung von Biomasse
CZ19731U1 (cs) * 2009-04-22 2009-06-15 Tuma@Stanislav Zarízení pro výrobu elektrické energie a tepla z biomasy

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

Also Published As

Publication number Publication date
DE112011104722A5 (de) 2013-11-07
EP2663742A2 (fr) 2013-11-20
WO2012095119A2 (fr) 2012-07-19
WO2012095119A3 (fr) 2013-04-18
DE202011001453U1 (de) 2011-05-05

Similar Documents

Publication Publication Date Title
EP2663742B1 (fr) Procédé et installation permettant la récupération d&#39;énergie à partir de la biomasse et des déchets combustibles, en particulier des matières premières renouvelables, ainsi que leur carbonisation
DE3049706C2 (de) Vorrichtung zur Behandlung von organischen Materialstücken in einer gasdicht verschließbaren Behandlungskammer
DE102006007458B4 (de) Verfahren und Vorrichtung zum Vergasen von kohlenstoffhaltigem Material sowie Vorrichtung zur Erzeugung von elektrischer Energie
DE68907052T2 (de) Verfahren und vorrichtung zur veredelung von organischem material.
ES2691722T3 (es) Planta modular para realizar procedimientos de conversión de matrices carbonáceas
DE2651302A1 (de) Verfahren fuer die umsetzung durch pyrolyse von abfall und vorrichtung zur durchfuehrung desselben
EP2424957A1 (fr) Dispositif, son utilisation, procédé et système pour la transformation en continu d&#39;une biomasse
DE2927240A1 (de) Verfahren und anlage zum vergasen von stueckigen brennstoffen
EP1377649B1 (fr) Installation et procede pour produire de l&#39;energie par pyrolyse
WO2008122279A2 (fr) Brûleur à combustible solide et procédé de refroidissement de ce brûleur
WO2009095015A1 (fr) Procédé de carbonisation de substances organiques
EP0360052A1 (fr) Réacteur de pyrolyse pour l&#39;élimination thermique de déchets
EP0765928B1 (fr) Générateur de gaz pour la production continue d&#39;un gaz combustible
WO2011079948A1 (fr) Dispositif de conversion continue de biomasse et système de production d&#39;énergie en résultant
DE102006007457B4 (de) Verfahren und Vorrichtung zum Erzeugen von Gas aus kohlenstoffhaltigem Material
AT9842U1 (de) Holzvergaser und verfahren zur verbrennung von hackschnitzeln und/oder pellets
DE202013105519U1 (de) Vorrichtung zur Herstellung von Brennstoffen zur energetischen Nutzung
DE69204948T2 (de) Methode und Vorrichtung zum Vergasen von festen Brennstoffen, enthaltend schmelzbare nicht-brennbare Materien.
DE3933576C1 (en) Extruding industrial sludge into pellets - increasing dry material content to over 70 per-cent, expelling water
EP0080549B1 (fr) Procédé pour la production d&#39;un gaz de pyrolyse à partir de matériaux combustibles et installation pour la mise en oeuvre du procédé
DE102005030096A1 (de) Energiewandlungssystem für feste Biomasse
WO2012110236A1 (fr) Production de carbone et de gaz combustibles à partir de lignite
EP3491312A1 (fr) Sécheur par contact
DE102006059485B4 (de) Holzvergaser, Verfahren zur Durchführung einer Holzvergasung und Anlage
DE202014007334U1 (de) Biomassevergasungsanlage

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20130709

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

DAX Request for extension of the european patent (deleted)
RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: GERHARD RIEDER GMBH

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20180213

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE PATENT HAS BEEN GRANTED

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: AT

Ref legal event code: REF

Ref document number: 1012544

Country of ref document: AT

Kind code of ref document: T

Effective date: 20180715

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: GERMAN

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 502011014373

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180927

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: NO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180927

REG Reference to a national code

Ref country code: NL

Ref legal event code: MP

Effective date: 20180627

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG4D

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180928

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20181027

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: PL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SM

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 502011014373

Country of ref document: DE

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20181211

Year of fee payment: 9

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

26N No opposition filed

Effective date: 20190328

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20190128

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190128

REG Reference to a national code

Ref country code: BE

Ref legal event code: MM

Effective date: 20190131

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190131

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190131

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190131

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190131

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190128

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190128

REG Reference to a national code

Ref country code: AT

Ref legal event code: MM01

Ref document number: 1012544

Country of ref document: AT

Kind code of ref document: T

Effective date: 20190128

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: TR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20190128

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20181029

REG Reference to a national code

Ref country code: DE

Ref legal event code: R119

Ref document number: 502011014373

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20200801

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HU

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO

Effective date: 20110128

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20180627